CN110845322A - Apparatus for producing methacrylic acid - Google Patents

Apparatus for producing methacrylic acid Download PDF

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CN110845322A
CN110845322A CN201911029108.2A CN201911029108A CN110845322A CN 110845322 A CN110845322 A CN 110845322A CN 201911029108 A CN201911029108 A CN 201911029108A CN 110845322 A CN110845322 A CN 110845322A
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reactor
max
line
outlet
ave
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CN110845322B (en
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须安范明
犬饲正二
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Sumitomo Chemical Co Ltd
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Sumitomo Chemical Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/25—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring
    • C07C51/252—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of unsaturated compounds containing no six-membered aromatic ring of propene, butenes, acrolein or methacrolein
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/16—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation
    • C07C51/21—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen
    • C07C51/23—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups
    • C07C51/235—Preparation of carboxylic acids or their salts, halides or anhydrides by oxidation with molecular oxygen of oxygen-containing groups to carboxyl groups of —CHO groups or primary alcohol groups
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0046—Sequential or parallel reactions, e.g. for the synthesis of polypeptides or polynucleotides; Apparatus and devices for combinatorial chemistry or for making molecular arrays
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
    • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
    • C07C45/33—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties
    • C07C45/34—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds
    • C07C45/35—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of CHx-moieties in unsaturated compounds in propene or isobutene
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/27—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation
    • C07C45/32—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen
    • C07C45/37—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups
    • C07C45/38—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by oxidation with molecular oxygen of >C—O—functional groups to >C=O groups being a primary hydroxyl group
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C47/00—Compounds having —CHO groups
    • C07C47/20—Unsaturated compounds having —CHO groups bound to acyclic carbon atoms
    • C07C47/21—Unsaturated compounds having —CHO groups bound to acyclic carbon atoms with only carbon-to-carbon double bonds as unsaturation
    • C07C47/22—Acryaldehyde; Methacryaldehyde
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C57/00—Unsaturated compounds having carboxyl groups bound to acyclic carbon atoms
    • C07C57/02—Unsaturated compounds having carboxyl groups bound to acyclic carbon atoms with only carbon-to-carbon double bonds as unsaturation
    • C07C57/03—Monocarboxylic acids
    • C07C57/04—Acrylic acid; Methacrylic acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00164—Controlling or regulating processes controlling the flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
    • B01J2219/00277—Apparatus
    • B01J2219/00279—Features relating to reactor vessels
    • B01J2219/00331—Details of the reactor vessels
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00274—Sequential or parallel reactions; Apparatus and devices for combinatorial chemistry or for making arrays; Chemical library technology
    • B01J2219/00277—Apparatus
    • B01J2219/00351—Means for dispensing and evacuation of reagents

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)

Abstract

The invention provides a methacrylic acid production apparatus capable of simplifying equipment. An apparatus for producing methacrylic acid, comprising: a first reactor (10); second reactor R1～Rn(n represents an integer of 2 or more); a Line (LA) associated with the outlet of the first reactor (10) and the second reactor R1～RnAnd the stream coming out of the outlet of the first reactor (10) is branched and fed to the second reactor R1～RnA respective inlet; and a Line (LB) which is connected to the second reactor R1～RnRespective outlets are connected and led from the second reactor R1～RnThe streams from the outlets of (a) are joined, a second reactor R1～RnHeight A of the bottom, second reactor R1～RnRespective height H from the branching of the Line (LA) to the second reactor R1～RnAnd from the second reactor R1～RnThe pipe in the flow path from the outlet of (b) to the junction of the Lines (LB) satisfies a predetermined condition.

Description

Apparatus for producing methacrylic acid
Technical Field
The present invention relates to a methacrylic acid production apparatus.
Background
Patent document 1 describes a method for producing methacrylic acid.
Documents of the prior art
Patent document
Patent document 1: international publication No. 2008/145417
Disclosure of Invention
Problems to be solved by the invention
The production apparatus used for producing methacrylic acid is preferably simple in equipment. Accordingly, an object of the present invention is to provide a methacrylic acid production apparatus capable of simplifying the facilities.
Means for solving the problems
The apparatus for producing methacrylic acid of the present invention comprises: a first reactor for obtaining methacrolein from isobutylene and/or tert-butanol (hereinafter referred to as "TBA") and oxygen; a plurality of second reactors R1～Rn(n represents an integer of 2 or more), and a plurality of second reactors R1～RnFor obtaining methacrylic acid by reacting methacrolein and oxygen; line LA with the outlet of the first reactor and the second reactor R1～RnAnd the stream coming out of the outlet of the first reactor is branched and fed to the second reactor R1～RnA respective inlet; and a line LB with the second reactor R1～RnRespective outlets are connected and led from the second reactor R1～RnIs combined with the outlet stream of (b) to a second reactor R1～RnHeight A of the respective bottom1～AnThe second reactor R is arranged so as to satisfy the formula (2)1～RnSecond reactor R1～RnEach height H1～HnSatisfies the formula (3), from the branch portion of the line LA to the second reactor R1～RnInlet R of1i～RniEach flow path C1i ℃Cni inner diameter D of the pipe1i～DniAnd length L1i～LniSatisfying the conditions of the formulae (4a) and (4b), from the second reactor R1～RnOutlet R of (2)1j～RnjInner diameters D of pipes in the respective flow paths C1j to Cnj to the junction of the line LB1j～DnjAnd length L1j～LnjThe conditions of the formulae (5a) and (5b) are satisfied.
(Amax-Amin)/Aave≤0.02(2)
[AmaxIs represented by A1～AnMaximum value of (1), AminIs represented by A1～AnMinimum value of (A)aveIs represented by A1～AnAverage value of (a).]
(Hmax-Hmin)/Have≤0.02(3)
[HmaxRepresents H1～HnMaximum value of (1), HminRepresents H1～HnMinimum value of (1), HaveRepresents H1～HnAverage value of (a).]
(Dmax(i)/Dmin(i))≤1.025(4a)
[Dmax(i)Represents D1i～DniMaximum value of (1), Dmin(i)Represents D1i～DniMinimum value of (1).]
(Lmax(i)/Lmin(i))≤1.05(4b)
[Lmax(i)Represents L1i～LniMaximum value of (1), Lmin(i)Represents L1i～LniMinimum value of (1).]
(Dmax(j)/Dmin(j))≤1.025(5a)
[Dmax(j)Represents D1j～DnjMaximum value of (1), Dmin(j)Represents D1j～DnjMinimum value of (1).]
(Lmax(j)/Lmin(j))≤1.05(5b)
[Lmax(j)Represents L1j～LnjMaximum value of (1), Lmin(j)Represents L1j～LnjMinimum value of (1).]
According to such an apparatus for producing methacrylic acid, facilities can be simplified.
In the apparatus for producing methacrylic acid, it is preferable that when the same fluid is passed through the flow paths C1i to Cni at the same flow rate, the pressure loss Δ P between the inlet and the outlet in each of the flow paths C1i to Cni is1i～ΔPniWhen the same fluid flows through the flow paths C1j to C Cnj at the same flow rate, the pressure loss Δ P between the inlet and the outlet of each of the flow paths C1j to C Cnj satisfies the formula (1a)1j～ΔPnjSatisfies the formula (1b),
(ΔPmax(i)-ΔPmin(i))/ΔPave(i)≤0.10(1a)
[ΔPmax(i)represents Δ P1i～ΔPniMaximum value of (1), Δ Pmin(i)Represents Δ P1i～ΔPniMinimum value of, Δ Pave(i)Represents Δ P1i～ΔPniAverage value of (2)]
(ΔPmax(j)-ΔPmin(j))/ΔPave(j)≤0.10(1b)
[ΔPmax(j)Represents Δ P1j～ΔPnjMaximum value of (1), Δ Pmin(j)Represents Δ P1j～ΔPnjMinimum value of, Δ Pave(j)Represents Δ P1j～ΔPnjAverage value of (2)]。
Thereby, the apparatus can be further simplified.
Effects of the invention
According to the present invention, an apparatus for producing methacrylic acid is provided, which can simplify facilities.
Drawings
Fig. 1 is a diagram showing an example of an apparatus for producing methacrylic acid according to the present embodiment.
Reference numerals
10 … a first reactor,
20 … second reactor,
50b … gas mixer,
60 … separation unit,
100 … apparatus for producing methacrylic acid
Detailed Description
In the present specification, isobutylene means 2-methylpropene.
First, an apparatus 100 for producing methacrylic acid according to the present embodiment will be described with reference to fig. 1. Fig. 1 is a diagram showing an example of an apparatus for producing methacrylic acid according to the present embodiment.
This production apparatus 100 is an example of a production apparatus in the case where the second reactor includes 2 reactors. That is, the manufacturing apparatus 100 is shown in a plurality of second reactors R1～Rn(n represents an integer of 2 or more) in the case where n is 2. In the explanation of the manufacturing apparatus 100, "A1～An”、“H1～Hn”、“D1i～Dni”、“L1i～Lni”、“D1j～Dnj”、“L1j～Lnj”、“ΔP1i～ΔPni"and" Δ P1j～ΔPnjThe "description" means "A" respectively1And A2”、“H1And H2”、“D1iAnd D2i”、“L1iAnd L2i”、“D1jAnd D2j”、“L1jAnd L2j”、“ΔP1iAnd Δ P2i"and" Δ P1jAnd Δ P2j”。
The manufacturing apparatus 100 mainly includes: a first reactor 10, a second reactor 20, a separation unit 60, and lines LA and LB. Line LA has a gas mixer 50 b. The second reactor 20 comprises a reactor R1And R2。
A supply source (S0) of a gas containing isobutylene and/or TBA and oxygen is connected to the inlet 10i of the first reactor 10 through a line L10.
The first reactor 10 is a reactor for obtaining methacrolein from isobutylene and/or TBA and oxygen.
The first reactor 10 is preferably a reactor in which a vessel is filled with a catalyst. The first reactor 10 may be a fixed bed reactor in which a catalyst is filled in a vessel. The direction of the flow is not limited and may be upward or downward. Examples of the catalyst used in the reaction for synthesizing methacrolein from isobutylene and/or TBA and oxygen are metal oxides containing molybdenum and bismuth.
In the case of obtaining methacrolein from isobutylene and oxygen, isobutylene reacts with oxygen, thereby producing methacrolein. TBA may also be used in place of isobutylene. When methacrolein is obtained from TBA and oxygen, it is considered that isobutylene is produced by dehydration reaction of TBA, and the produced isobutylene reacts with oxygen to produce methacrolein. The reason why TBA can be used instead of isobutylene is considered to be that the oxidation reaction of isobutylene in the first reactor 10 is a rate-limiting step. Isobutylene and TBA may also be used in combination.
The outlet 10j of the first reactor 10 and the inlet R of the second reactor 201iAnd R2iConnected by line LA. Inlet R of the second reactor 201iAnd R2iAre respectively a reactor R1And R2Of the inlet of (a). Line LA branches off the stream exiting from the outlet 10j of the first reactor 10 and feeds it to the reactor R1And R2The respective inlet lines.
Line L22 and inlet 50b of gas mixer 50b of line LAmAnd (4) connecting. The line L22 is a line connecting the line LA and the oxygen gas supply source (S1), and a compressor 55 is provided in a part of the line.
The second reactor 20 is a reactor for obtaining methacrylic acid by reacting methacrolein and oxygen. The reactor constituting the second reactor 20 is preferably a reactor in which a catalyst is filled in a vessel. The reactor constituting the second reactor 20 may be a fixed bed reactor in which a catalyst is filled in a vessel. The fixed bed reaction apparatus may be, for example, an apparatus in which each tube of a multi-tube heat exchanger is packed with solid particles containing catalyst particles and, if necessary, inactive particles. The direction of the flow is not limited and may be upward or downward. Examples of the catalyst used in the reaction for synthesizing methacrylic acid from methacrolein and oxygen are heteropoly acid compounds containing phosphorus and molybdenum.
Outlet R of the second reactor 201jAnd R2jIs connected to the inlet 60i of the separation unit 60 via line LB. Outlet R of the second reactor 201jAnd R2jAre respectively a reactor R1And R2An outlet of (3). Line LB is for the secondary reactor R1And R2The streams exiting the outlets of which are combined and fed to the lines of the separation unit 60.
At a height A of the respective bottom1And A2The reactor R is arranged so as to satisfy the formula (2)1And R2. Reactor R1And R2Each height H1And H2Satisfies the formula (3). Here, the height refers to a length in the vertical direction. The height a of the bottom of the reactor refers to the height from the ground to the bottom of the reactor, and the height H of the reactor refers to the height of the reactor itself.
(Amax-Amin)/Aave≤0.02(2)
[AmaxIs represented by A1～AnMaximum value of (1), AminIs represented by A1～AnMinimum value of (A)aveIs represented by A1～AnAverage value of (a).]
(Hmax-Hmin)/Have≤0.02(3)
[HmaxRepresents H1～HnMaximum value of (1), HminRepresents H1～HnMinimum value of (1), HaveRepresents H1～HnAverage value of (a).]
AaveFor example, it may be 1m to 15m, 2m to 12m, or 4m to 10 m.
HaveFor example, it may be 1m to 12m, 2m to 10m, or 4m to 8 m.
From the branch Xa of the line LA to the reactor R1Inlet R of1iInner diameter D of the pipe in the flow path C1i of (2)1iAnd length L1iAnd fromThe branch Xa of the line LA leads into the reactor R2Inlet R of2iInner diameter D of the pipe in the flow path C2i2iAnd length L2iThe conditions of the formulae (4a) and (4b) are satisfied.
(Dmax(i)/Dmin(i))≤1.025(4a)
[Dmax(i)Represents D1i～DniMaximum value of (1), Dmin(i)Represents D1i～DniMinimum value of (1).]
(Lmax(i)/Lmin(i))≤1.05(4b)
[Lmax(i)Represents L1i～LniMaximum value of (1), Lmin(i)Represents L1i～LniMinimum value of (1).]
From reactor R1Outlet R of (2)1jInner diameter D of conduit in flow path C1j to confluence Xb of line LB1jAnd length L1jWith a secondary reactor R2Outlet R of (2)2jInner diameter D of conduit in flow path C2j to junction Xb of line LB2jAnd length L2jThe conditions of the formulae (5a) and (5b) are satisfied.
(Dmax(j)/Dmin(j))≤1.025(5a)
[Dmax(j)Represents D1j～DnjMaximum value of (1), Dmin(j)Represents D1j～DnjMinimum value of (1).]
(Lmax(j)/Lmin(j))≤1.05(5b)
[Lmax(j)Represents L1j～LnjMaximum value of (1), Lmin(j)Represents L1j～LnjMinimum value of (1).]
In the present specification, the inner diameter of the pipe means an average value of integrals in the length direction of the inner diameter of the pipe. The length of the pipe means the length of the central axis of the pipe.
Dmax(i)For example, it may be 200mm to 1800mm, 400mm to 1500mm, or 600mm to 1300 mm.
Lmax(i)For example, it may be 1m to 40m, or 5m to E35m, and may be 10 to 30 m.
Dmax(j)For example, it may be 200mm to 1800mm, 400mm to 1500mm, or 600mm to 1300 mm.
Lmax(j)For example, the thickness may be 1m to 40m, 5m to 35m, or 10m to 30 m.
From the viewpoint of facilitating further simplification of the facility, the manufacturing apparatus 100 preferably includes: when the same fluid is passed at the same flow rate in the flow paths C1i and C2i, the pressure loss Δ P between the inlet and the outlet in the flow path C1i1iAnd pressure loss Δ P between the inlet and the outlet in the flow path C2i2iSatisfying the formula (1a), when the same fluid is passed at the same flow rate in the flow paths C1j and C2j, the pressure loss Δ P between the inlet and the outlet in the flow path C1j1jAnd pressure loss Δ P between the inlet and the outlet in the flow path C2j2jSatisfies the formula (1 b). Herein, the same fluid means a fluid having the same composition, temperature and pressure.
(ΔPmax(i)-ΔPmin(i))/ΔPave(i)≤0.10(1a)
[ΔPmax(i)Represents Δ P1i～ΔPniMaximum value of (1), Δ Pmin(i)Represents Δ P1i～ΔPniMinimum value of, Δ Pave(i)Represents Δ P1i～ΔPniAverage value of (a).]
(ΔPmax(j)-ΔPmin(j))/ΔPave(j)≤0.10(1b)
[ΔPmax(j)Represents Δ P1j～ΔPnjMaximum value of (1), Δ Pmin(j)Represents Δ P1j～ΔPnjMinimum value of, Δ Pave(j)Represents Δ P1j～ΔPnjAverage value of (a).]
From the branch part Xa to the reactor R1Inlet R of1iFlow path C1i from branch part Xa to reactor R2Inlet R of2iThe flow path C2i may be substantially the same in shape. This tends to make the manufacturing apparatus 100 easily satisfy the range of formula (1 a). From reactor R1Outlet R of (2)1jTo meetFlow path C1j of section Xb and secondary reactor R2Outlet R of (2)2jThe flow path C2j to the junction Xb may be substantially the same in its shape. This tends to make the manufacturing apparatus 100 easily satisfy the range of formula (1 b). The shape of the duct included between the branch part Xa and the junction part Xb may be substantially symmetrical with respect to any one of the planes including the line connecting the branch part Xa and the junction part Xb.
The separation unit 60 discharges a stream containing carbon monoxide, carbon dioxide, nitrogen, argon, light components and oxygen from a first outlet (F35), a stream containing methacrylic acid and heavy components from a second outlet (F31), and a stream containing methacrolein from a third outlet (F23). Line L35 is connected to the first outlet, line L31 is connected to the second outlet, and line L23 is connected to the third outlet.
Line L23 is connected to line LA.
Examples of the separation unit 60 include: distillation columns, extraction columns, absorption columns, and combinations thereof. In case the separation unit 60 comprises one distillation column, it is preferred that: the line L35 was disposed at the upper part of the distillation column, the line L31 was disposed at the lower part of the distillation column, and the line L23 was disposed at the side of the distillation column.
Next, a method for producing methacrylic acid according to the present embodiment will be described.
(supply source)
A stream (F10) containing isobutylene and/or TBA and oxygen is prepared as a supply source (S0) of a gas containing isobutylene and/or TBA and oxygen.
The stream (F10) may contain constituents other than isobutylene, TBA and oxygen. Examples of the components other than isobutylene, TBA and oxygen include: c5 olefins such as isoprene, isobutane, 1-butene, 2-butene (cis, trans), propane, propylene, n-butane, methyl tert-butyl ether, methanol, dimethyl ether, butadiene, propadiene, diisobutylene, nitrogen, carbon dioxide, carbon monoxide, water and argon.
The concentration of isobutene and/or TBA in the stream (F10) is, for example, 1 mass% or more, 2 mass% or more or 4 mass% or more, based on the sum of the concentrations of isobutene and TBA. The sum of the concentrations of isobutene and TBA in the stream (F10) is, for example, 21 mass% or less, 19 mass% or less, or 17 mass% or less. The sum of the concentrations of isobutylene and TBA in the stream (F10) is preferably 1 to 21 mass%, more preferably 2 to 19 mass%, and further preferably 4 to 17 mass%.
The oxygen concentration in the stream (F10) is, for example, 7 mass% or more, 8 mass% or more, or 10 mass% or more. The oxygen concentration in the stream (F10) is, for example, 24 mass% or less, 23 mass% or less, or 21 mass% or less. The oxygen concentration in the stream (F10) is preferably 7 to 24 mass%, more preferably 8 to 23 mass%, and still more preferably 10 to 21 mass%.
In addition, an oxygen-containing stream (F22) as an oxygen supply source (S1) was prepared.
The oxygen concentration in the stream (F22) is, for example, 15 mass% or more. The oxygen concentration in the stream (F22) is preferably 16% by mass or more, more preferably 17% by mass or more, and further preferably 20% by mass or more. The upper limit of the oxygen concentration in the stream (F22) may be set, for example, to 35 mass%. The oxygen concentration in the stream (F22) may be, for example, 30 mass% or less, or may be 25 mass% or less. The oxygen concentration in the stream (F22) is preferably 16 to 35 mass%, more preferably 17 to 30 mass%, and still more preferably 18 to 25 mass%.
(reaction procedure)
Stream (F10) is fed to first reactor 10, where isobutylene and oxygen in stream (F10) are reacted in first reactor 10. A stream (F11) containing methacrolein obtained by the reaction of isobutylene and oxygen was discharged from the line LA.
The reaction temperature of the first reactor 10 may be set to 300 to 400 ℃. The reaction pressure of the first reactor 10 may be set to 0.004MPaG to 0.6MPaG (gauge pressure).
A methacrolein-containing stream (F23) is mixed in the stream (F11) discharged from the first reactor 10 through a line L23 and an oxygen-containing stream (F22) is mixed through a line L22. The stream (F) thus obtained21) Is fed to each reactor (R) of the second reactor 20 via line LA1And R2)。
The concentration of methacrolein in the stream (F23) is preferably 0.1% by mass or more, more preferably 3% by mass or more, further preferably 7% by mass or more. The concentration of methacrolein in the stream (F23) is preferably 32% by mass or less, more preferably 23% by mass or less, further preferably 16% by mass or less. The concentration of methacrolein in the stream (F23) may be from 0.1% by mass to 32% by mass, may also be from 3% by mass to 23% by mass, and may also be from 7% by mass to 16% by mass. Stream (F23) may contain, for example, nitrogen, water and carbon dioxide as components other than methacrolein.
In the second reactor 20, methacrolein and oxygen are reacted to obtain methacrylic acid, and a stream containing methacrylic acid is discharged through a line LB (F30).
Stream (F30) typically contains unreacted methacrolein. Stream (F30) may contain components other than methacrylic acid and methacrolein. Examples of such components include: acrylic acid, acrolein, nitrogen, argon, oxygen, water, carbon monoxide, carbon dioxide, acetaldehyde, propionaldehyde, terephthalic acid, maleic acid, fumaric acid, diacetyl, isophthalic acid, isobutyric acid, methylfurfural, acetic acid, propionic acid, and the like.
The reaction temperature of the second reactor 20 may be set to 200 to 350 ℃. The reaction pressure in the second reactor 20 is, for example, 0.01MPaG to 0.3 MPaG.
(separation step and Recycling step)
Stream (F30) is supplied to separation unit 60 via line LB. The streams are separated in the separation unit 60, a stream comprising carbon monoxide, carbon dioxide, nitrogen, argon, light components and oxygen being withdrawn from line L35 (F35), a stream comprising methacrylic acid and heavy components being withdrawn from line L31 (F31), and a stream comprising methacrolein being withdrawn from line L23 (F23).
The methacrolein-containing stream (F23) was joined to the stream (F11) through a line L23.
Methacrylic acidThe acid production apparatus 100 includes: a first reactor 10, the first reactor 10 being used for obtaining methacrolein from isobutene and/or TBA and oxygen; a plurality of second reactors 20 (R)1And R2) A plurality of second reactors 20 for obtaining methacrylic acid by reacting methacrolein and oxygen; line LA communicating with the outlet 10j of the first reactor 10 and the second reactor 20 (R)1And R2) And a stream coming out of the outlet 10j of the first reactor 10 is branched and supplied to the second reactor 20 (R)1And R2) A respective inlet; and a line LB, which is connected to the second reactor 20 (R)1And R2) Respective outlets are connected and led from the second reactor 20 (R)1And R2) Is combined with the outlet of the reactor R1And R2Height A of the respective bottom1And A2The reactor R is arranged so as to satisfy the formula (2)1And R2Reactor R1And R2Each height H1And H2Satisfying the formula (3), from the branch Xa of the line LA to the reactor R1And R2Inlet R of1iAnd R2iRespectively flow paths C1i and C2i, and an inner diameter D of the pipe1iAnd D2iAnd a length L1iAnd L2iSatisfying the conditions of formula (4a) and formula (4b), from reactor R1And R2Outlet R of (2)1jAnd R2jInner diameter D of the tube in each of flow paths C1j and C2j to the junction Xb of the line LB1jAnd D2jAnd a length L1jAnd L2jThe conditions of the formulae (5a) and (5b) are satisfied. Thus, it is considered that even if no valve or the like is provided in the line LA, the fluid can easily flow uniformly through the reactor R1And R2Therefore, the apparatus can be simplified and can be stably operated for a long period of time even without performing a particularly complicated operation. Further, since a valve or the like is not necessarily required at the above position, it is considered that clogging of a pipe or the like at a site having a complicated shape such as a valve can be prevented. Further, since the apparatus for producing methacrylic acid 100 has a plurality of second reactors, it is likely that the amount of the catalyst in the second reactor is larger than necessary.It is considered that by filling the amount of catalyst of the second reactor more than necessary, for example, even in the case where the catalyst activity of the second reactor is reduced earlier than that of the first reactor, the productivity of the second reactor is easily maintained.
It is considered that the apparatus of the present embodiment is excellent in continuous operability, and therefore can reduce raw materials and energy during long-term operation.
The present invention is not limited to the above embodiment, and various modifications are possible.
For example, a separation and purification unit such as a distillation column or an extraction column may be further added to each line.
The gas mixer 50b may be omitted. In this case, the line L22 may be directly connected with the pipe of the line L21.
Line L23 may be present or line L23 may not be present. In the apparatus 100 for producing methacrylic acid, the line L23 is connected to the separation unit 60, but the line L23 may not be connected to the separation unit 60. That is, the stream supplied to line LA through line L23 may not be a recycle stream from separation unit 60.
The second reactor may be composed of three or more reactors. I.e. in a plurality of second reactors R1～RnIn (e), n may be 3 or more. In this case, the branch portion of the line LA branches into n flow paths, and the n flow paths merge at the merging portion of the line LB. Further, the following means may be used: at a height A of the respective bottom1～AnThe reactor R is arranged so as to satisfy the formula (2)1～RnAnd reactor R1～RnHeight H of1～HnSatisfying the formula (3), from the branching portion of the line LA to the reactor R1～RnInlet R of1i～RniInner diameters D of the pipes in the respective flow paths C1i to Cni1i～DniAnd length L1i～LniSatisfying the conditions of formula (4a) and formula (4b), from reactor R1～RnOutlet R of (2)1j～RnjInner diameters D of pipes in the respective flow paths C1j to Cnj to the junction of the line LB1j～DnjAnd length L1j～LnjThe conditions of the formulae (5a) and (5b) are satisfied.
Even when n is 3 or more, it is preferable that: when the same fluid flows through the flow paths C1i to Cni at the same flow rate, the pressure loss Δ P between the inlet and the outlet of each of the flow paths C1i to Cni is1i～ΔPniWhen the same fluid flows through the flow paths C1j to C Cnj at the same flow rate, the pressure loss Δ P between the inlet and the outlet of each of the flow paths C1j to C Cnj satisfies the formula (1a)1j～ΔPnjSatisfies the formula (1 b).

Claims (2)

1. An apparatus for producing methacrylic acid, comprising:
a first reactor for obtaining methacrolein from isobutylene and/or tert-butanol and oxygen;
a plurality of second reactors R1～RnSaid plurality of second reactors R1～RnFor obtaining methacrylic acid by reacting methacrolein with oxygen, n represents an integer of 2 or more;
line LA with the outlet of the first reactor and the second reactor R1～RnAnd the stream coming out of the outlet of the first reactor is branched and fed to the second reactor R1～RnA respective inlet; and
line LB with a second reactor R1～RnRespective outlets are connected and led from the second reactor R1～RnThe streams coming out of the outlets of the two flow paths are merged,
with a second reactor R1～RnHeight A of the respective bottom1～AnThe second reactor R is arranged so as to satisfy the formula (2)1～Rn，
Second reactor R1～RnEach height H1～HnSatisfies the formula (3),
from the branch of line LA to the second reactor R1～RnInlet R of1i～RniInner diameters D of the pipes in the respective flow paths C1i to Cni1i～DniAnd length L1i～LniSatisfying the conditions of the formula (4a) and the formula (4b),
from the second reactor R1～RnOutlet R of (2)1j～RnjInner diameters D of pipes in the respective flow paths C1j to Cnj to the junction of the line LB1j～DnjAnd length L1j～LnjSatisfying the conditions of the formula (5a) and the formula (5b),
(Amax-Amin)/Aave≤0.02 (2)
Amaxis represented by A1～AnMaximum value of (1), AminIs represented by A1～AnMinimum value of (A)aveIs represented by A1～AnAverage value of (d);
(Hmax-Hmin)/Have≤0.02 (3)
Hmaxrepresents H1～HnMaximum value of (1), HminRepresents H1～HnMinimum value of (1), HaveRepresents H1～HnAverage value of (d);
(Dmax(i)/Dmin(i))≤1.025(4a)
Dmax(i)represents D1i～DniMaximum value of (1), Dmin(i)Represents D1i～DniMinimum value of (1);
(Lmax(i)/Lmin(i))≤1.05(4b)
Lmax(i)represents L1i～LniMaximum value of (1), Lmin(i)Represents L1i～LniMinimum value of (1);
(Dmax(j)/Dmin(j))≤1.025(5a)
Dmax(j)represents D1j～DnjMaximum value of (1), Dmin(j)Represents D1j～DnjMinimum value of (1);
(Lmax(j)/Lmin(j))≤1.05(5b)
Lmax(j)represents L1j～LnjMaximum value of (1), Lmin(j)Represents L1j～LnjMinimum value of (1).
2. The apparatus for producing methacrylic acid according to claim 1, wherein when the same fluid is passed through the flow paths C1i to C Cni at the same flow rate, the pressure loss Δ P between the inlet and the outlet of each of the flow paths C1i to C Cni is1i～ΔPniSatisfies the formula (1a),
when the same fluid flows through the flow paths C1j to Cnj at the same flow rate, the pressure loss Δ P between the inlet and the outlet of each of the flow paths C1j to Cnj is1j～ΔPnjSatisfies the formula (1b),
(ΔPmax(i)-ΔPmin(i))/ΔPave(i)≤0.10(1a)
ΔPmax(i)represents Δ P1i～ΔPniMaximum value of (1), Δ Pmin(i)Represents Δ P1i～ΔPniMinimum value of, Δ Pave(i)Represents Δ P1i～ΔPniAverage value of (d);
(ΔPmax(j)-ΔPmin(j))/ΔPave(j)≤0.10(1b)
ΔPmax(j)represents Δ P1j～ΔPnjMaximum value of (1), Δ Pmin(j)Represents Δ P1j～ΔPnjMinimum value of, Δ Pave(j)Represents Δ P1j～ΔPnjAverage value of (a).
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CN101133014A (en) * 2005-03-01 2008-02-27 巴斯福股份公司 Process for preparing at least one organic target compound by heterogeneously catalyzed gas phase partial oxidation

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